化工原理乙醇水課程設(shè)計(jì)

1、化工原理課程設(shè)計(jì)別離乙醇-水混合物精偕塔設(shè)計(jì)學(xué) 院：化學(xué)工程學(xué)院專 業(yè)：學(xué) 號(hào)：姓 名：指導(dǎo)教師:時(shí)間：2021 年6月13日星期三化工原理課程設(shè)計(jì)任務(wù)書一、設(shè)計(jì)題目：別離乙醇-水混合物精僻塔設(shè)計(jì)二、原始數(shù)據(jù)：a 原料液組成：乙醇20 % 產(chǎn)品中：乙醇含量英4% 殘液中M%b生產(chǎn)水平：6萬噸/年c操作條件進(jìn)料狀態(tài)：自定操作壓力：自定加熱蒸汽壓力：自定冷卻水溫度：自定三、設(shè)計(jì)說明書內(nèi)容：a概述b流程確實(shí)定與說明c 塔板數(shù)的計(jì)算板式塔；或填料層高度計(jì)算填料塔d塔徑的計(jì)算e1塔板結(jié)構(gòu)計(jì)算；a塔板結(jié)構(gòu)尺寸確實(shí)定；b塔板的流體力學(xué)驗(yàn)算；c塔板的負(fù)荷性能圖2填料塔流體力學(xué)計(jì)算；a壓力降；b噴淋密度計(jì)算f

2、其它1熱量衡算一冷卻水與加熱蒸汽消耗量的計(jì)算2冷凝器與再沸器傳熱面的計(jì)算與選型板式塔3除沫器設(shè)計(jì)g料液泵的選型h計(jì)算結(jié)果一覽表第一章 課程設(shè)計(jì)報(bào)告內(nèi)容一、精僻流程確實(shí)定乙醇、水混合料液經(jīng)原料預(yù)熱器加熱至泡點(diǎn)后,送入精僻塔.塔頂上升蒸汽采用全凝器 冷凝后,一局部作為回流,其余為塔頂產(chǎn)品經(jīng)冷卻器冷卻后送至貯槽.塔釜采用間接蒸 汽向沸熱器供熱,塔底產(chǎn)品經(jīng)冷卻后送入貯槽.二、塔的物料衡算一料液及塔頂、塔底產(chǎn)品含乙醇摩爾分?jǐn)?shù)Xf20/4620/46 80/18=0.089294/46Xd = =0.8694/46 6/184/46x = = 0.0164/46 96/18二平均摩爾質(zhì)量M F = 0.0

3、892 46 (1 - 0.0892) 18kg / kmol = 20.498kg / kmolMd =0.86 46 (1 -0.86) 18kg/ kmol = 42.08kg/ kmolMW =0.016 46 (1 -0.016) 18kg /kmol = 18.448kg / kmol(三) 物料衡算總物料衡算D W =F易揮發(fā)組分物料衡算Xd D XwW = Xf FD =mMd叮60000 100042.08 300 24kmol / h = 198.04kmol / h聯(lián)立以上三式得F =2283.41kmol/hW =2283.41kmol/h三、塔板數(shù)確實(shí)定一理論塔板數(shù)N

4、t的求取根據(jù)乙醇、水的氣液平衡數(shù)據(jù)作 y-x圖乙醇一水氣液平衡數(shù)據(jù)2.乙醇一水體系的平衡曲線有下凹局部,求最小回流比自a ( Xd,Xd,)作平衡線的切線并延長(zhǎng)與y軸相交,截距 日&+ =0.2956Rmin =1.91取操作回流比 R2Rmi2 1.91=3.82故精僻段操作線方程y =R 1 R 1即 y =0.7925x 0.17843.作圖法求理論塔板數(shù)Nt得Nt =18 不包括再沸器.第16層為加料板.四物性參數(shù)和實(shí)際塔板數(shù)的計(jì)算4.1溫度常壓下乙醇一水氣液平衡組成與溫度的關(guān)系溫度TC液相中乙醇的摩爾分率 氣相中乙醇的摩爾分率 1000.000.0095.50.01900.17008

5、9.00.07210.389186.70.09660.437585.30.12380.470484.10.16610.508982.70.23370.544582.30.26080.558081.60.32730.582680.70.39650.612279.80.50790.0656479.70.51980.659979.30.57320.684178.740.67630.738578.410.74720.781578.150.89430.8943利用表中數(shù)據(jù)由內(nèi)差可求得t F tD t W8986.7 = tf 89.0t F :7.21 -9.66 8.92 -7.21 78.15-78

6、.41 = td78.1589.43-74.42 86.0-89.43100 -95.5 = tw1000 -1.901.60t f=87.39 Ct d =78.21 Ct w=96.21 C 精儲(chǔ)段平均溫度：f1=5=87.39+78.21 =82.8 C22tf tw 87.39 96.21 提留段平均溫度 :t 2 =91.8 C塔頂溫度：td=78.21 C氣相組成yD78.41 78.1578.21 -78.15d=0.86830.7815 -0.8943yD -0.8943進(jìn)料溫度：t f=87.39 C89.0 -86.7氣相組成VR0.3891 -0.437589.0 87.

7、39f=0.42300.3891 - yF塔底溫度：t w=99.91 C氣相組成yw95.5 -89.095.591.8w=0.049230.019 -0.07210.019 - yw(1)精儲(chǔ)段液相組成XDXF氣相組成xi: x1 =2yD yF0.86 0.0892 =0.4746yr y1 =20.8683 0.4230 = 0.6457所以 Mli=46 0.4746 18 (1 -0.4746) =31.29kg / molMvi =46 0.6457 18 (1 - 0.6457) = 36.08kg / mol(2)提留段液相組成氣相組成XW - XFX2: X2 三2ywyF

8、0.016 0.0892 =0.0526y2: y2 =20.04923 0.04230=0.23614.2氣液組成所以 Ml2 =46 0.4746 18 (1 -0.4746) = 19.47kg / molMv2=46 0.2361 18 (1 -0.2361) =24.61kg / mol4.3液體粘度一乙醇的粘度1,塔頂溫度：t2,進(jìn)料溫度：t3,塔底溫度：t二水的黏度 1,塔頂溫度：td=78.21 Cf=87.39 Cw=99.91 Cd=78.21 C79 -7878.21-780.3160 -0.36552,進(jìn)料溫度：t88870.3239 -0.32763,塔底溫度：t97

9、96查表,查表,查表,乙醇=0.45mpa s,乙醇=0.38mpa s,乙醇=0.335mpa s,H2O -0.3655f=87.39 C87.39 -87H20 -0.3276w=99.91 C96.21-970.2930 -0.2962H2.-0.29624),nLm = 、Xii日F.LH2O =0.3551 ma sJo =0.3262 ma sH2o =0.2955 m？a s= 0.86 0.45 1 -0.86 0.3551 = 0.4367 m？a s= 0.38 0.0892 1-0.0892 0.3262 = 0.3310mM s= 0.335 0.016 1-0.01

10、6 0.2955 = 0.296lm？a s5)全塔平均液相黏度為0.4367 0.3310 0.2961=0.3546 ma s4.4相對(duì)揮發(fā)度由 x f=0.0892 y f=0.4230得aF0.4230/0.0892 小 = 7.491 -0.4230 / 1 -0.0892由 x d=0.86 y d=0.086830.8683/0.86得 aD = =1.071 -0.8683 / 1 -0.86由 xw=0.016 y w=0.049233.180.04923/0.0161 -0.04923 / 1 -0.0164.5全塔效率的估算(1) 用Oconenell對(duì)全塔效率進(jìn)行估算:

11、m = d：F：w- = j7.49 1.07 3.18 =5.05全塔平均液相黏度為0.4367 0.3310 0.2961= 0.3546 m？a s2全塔效率 ET =0.49(項(xiàng)、)Q245 =0.49 (5.05 0.3546)項(xiàng).245 43%(2) 實(shí)際塔板數(shù)Np庫專=房=42塊其中,精儲(chǔ)段的塔板數(shù)為：15/0.43 = 35塊4.6操作壓力(1) 操作壓力計(jì)算塔頂操作壓力 PD = 101.3 kPa每層塔板壓降 P= 0.7 kPa進(jìn)料板壓力 PF = 101.3 + 0.7 X 15= 125.72kPa塔底操作壓力 咒=101.3 + 0.7 X 42= 130.7kPa

12、精、均壓力Pm13 125.72 =113.5 kPa2提僻段平均壓力Pm2 =130.7 125.72= 128.21 kPa(2)密度乙醇與水的密度山東理工大學(xué)大學(xué)化學(xué)工程學(xué)院化工原理課程設(shè)計(jì)217溫度/ c2030405060708090100110乙醇密度/kg/m 3795785777765755746735730716703水密度/kg/m 3998.2995.7992.2988.1983.2977.8971.8965.3958.4951.0：1/ Pl_m =Ua/PlA +Ub/PlB(0(為質(zhì)量分?jǐn)?shù))1,液相密度 塔頂 由于t d =78.21 C80 -7078.21 -7

13、0所以=742.3 -754.2Leceoh - 754.23？ CH 3CH 2OH =731.31kg/m80 -7078.21 -70971.8 -977.8 一 *2.- 977.8孔 2O = 972.87kg/m310.940.06=十？d744.43 972.87進(jìn)料板由于tF =87.39 C90 -8087.37 -80所以=730 -735？ch3CH2Oh 一 735七=755.07 kg /m33？ CH 3CH 2OH =731.31kg/m90 -8087.39 -80730 -735 一 ：H2O 一735-一一一 一3,H2O = 966.77kg/m10.20

14、 1-0.20=r 七731.31966.77(3)塔釜由于 tW=96.21 C一3：F =908.30kg/m所以100一9=96.21-9717.3 -730.1Rh3ch2oh -730.13CH 3CH 2OH - 722.21 kg / m100 -90_ 96.21-90958.4 965.3 七2.一 965.3、2.=961.02kg/m310.016 1-0.016= J :W 722.21961.02：w -955.96 kg/m3(4)精僻段平均液相密度：L1 二1 755.07 908.30 = 831.69kg/m3山東理工大學(xué)大學(xué)化學(xué)工程學(xué)院化工原理課程設(shè)計(jì)1Q(

15、5)精僻段平均敝相密度Pl2 =(955.96+ 908.30) = 932.13kg/m32.氣相密度PmlM V1 1 =RT(1) 精僻段 ,3=1.38kg / m113.51 36.088.314 (82.80 273.15)(1)提僻段;V2Pm2Mv2RT128.21 24.618.314 (91.80 273.15),_ .,3=1.04kg / m504.7液體外表張力所以80 -7078.21 -7017.15-18 Lch3CH2Oh -18二CH3CH2OH - 17.3mN /m80 -70 _ 78.21-7062.6 -64.3 一 oH2O -64.3Fo =6

16、2.90mN /m進(jìn)料板由于tF =87.39 C所以90 -8016.2 -17.1587.39 -8064 3ch 3CH 2OH2-CH3CH2OH =16.45mN/m乙醇外表張力:溫度,c2030405060708090100110b , m N/m22.321.220.419.818.81817.1516.215.214.4水外表張力溫度,c020406080100b , m N/m75.6472.7569.6066.2462.6758.91 塔頂 由于t d =78.21 CTo =62.21mN /m90 -80 二 87.39 一8060.7 -62.6？H2O -62.6(

17、3) 塔釜由于t w=96.21 C100 -9096.21 -90所以=15.2-16.2LH3CH2OH -16.2-CH3CH2QH =15.58mN /m100 -9096.21 -9058.8 - 60.7 一 fo -60.7fo =59.52mN /m(4) 塔頂外表張力bd =0.86x17.3 + (1 -0.8662.21 = 58.13mN/m(6) 塔底外表張力而=0.016x15.58 + (10.016)x69.52=58.82mN/m(7) 精僻段平均外表張力.1 =】(23.68 + 58.13)=40.90mN/m2(8) 提僻段平均外表張力.2 =1(58.

18、82 + 58.13) = 40.90mN/m五、氣液負(fù)荷計(jì)算(1)精僻段V =(R 1)D =(3.82 1) 198.04 =954.55kmol/hVMV1 954.55 36.083V1 = 6.932m /s3600 1.383600,：V1L= RD =3.82 198.04 = 756.51kmol/hLM L1 756.51 31.29LS =36001 = 3600831.69 =0.00791m /s3Lh = LS 3600 = 0.00791 3600 = 28.46m / h(1)提僻段V =V = 954.55kmol / hVMv2 954.55 24.613,=

19、6.274m3/s3600 1.043600 % 2L= L qF = 3039.92kmol /hL M L2 3039.92 19.47LS =3600 = 3600932.13 =0.00176m /s3 = LS 3600 = 63.36m /h六、塔和塔板主要工藝尺寸計(jì)算一塔的有效高度計(jì)算初選板間距HT=0.40m,那么由公式 Z= NT -1 Ht = 迫-10.45 = 18.38mEt0.43二塔徑D參考表4-1,初選板間距Ht =0.45m,取板上液層高度hL = 0.07m表4-1板間距與塔徑的關(guān)系塔徑D/m0.3 -0.50.5 0.80.8 -1.61.6 2.42.4

20、 -4.0板間距H/mm200 -300250350300 -450350600400 -6001精僻段塔經(jīng)計(jì)算Ht -hT =0.45 -0.07 = 0.38m1= 0.0297LS 10.0079831.69 2廣)2 =Vsv. 6.932. 1.38圖4-5 Sminth 關(guān)聯(lián)圖查圖4-5可知,C2o=0.08,依照下式校正C0.2-、o.2 i40.09 :5C = C20 ()=0.08 =0.09220. 20Umax = CL1 _ V1 =0.09 七1831.69-1.38,2.26m/s1.38取平安系數(shù)為0.60,那么u =0.60umax =0.6 2.26 =1.

21、36m/s故D4 6.9323.14 1.36=2.55m按標(biāo)準(zhǔn),塔徑圓整為2.6m,塔截面積為 At = D2 =0.785 2.62 =5.31m24實(shí)際空塔氣速為魚=7=1.33m/sAt5.31提留段塔徑計(jì)算1橫坐標(biāo)數(shù)值：如*七 袂 心 0.077VS：V6.8691.04取板間距：Ht=0.45m , h L=0.07m .貝U Ht- h L=0.38m查圖可知G=0.078 ,-.158.48 02C =C20-1 =0.078 - .=0.0967 2020932.13二 1.04一umax =0.09672.89m / s1.04取平安系數(shù)為0.6那么空塔氣速 u1 =0.6

22、 umax =06 =2.89m/sD2=, 4VS2： u24 6.274=2.15m-：1.73按標(biāo)準(zhǔn)塔徑圓整后為 D2=2.6m綜上：塔徑D=2.6m,選擇雙流型塔板,截面積At = 5.31m2三溢流裝置采用單溢流、弓形降液管、平行受液盤及平行溢流堰,不設(shè)進(jìn)口堰.各項(xiàng)計(jì)算如下圖5-3塔板溢流;類型江型流 單溢淹 h雙溢麻 3階梯式抵溢流1.溢流堰長(zhǎng)lw單溢流 lw為 0.6D,即 lw =0.66=1.56m2.出口堰高h(yuǎn)whw = - how由 lw/D =1.56/2.6 =0.6 ,(1)精僻段Lh2.528.461.562.5= 9.36Wl；5查圖4-9,知E =1圖4-9液

23、流收縮系數(shù)計(jì)算圖2.84 匚 Lhlw )那么頑忌E22.84 ,28.46 310.02m1.561000故 hW =0.07 -0.02 = 0.05m(2)提僻段LhlW.563.36一 =20.841.56查圖4-9,知E =12.84 匚 howE1000lw2縫 1 63.36 0.03m10001.56故 hw =0.07 _0.03m =0.04m3.弓形降液管滴面積由 lw/D =0.65 0-4 0.30/20.020.1 O 08 Q O& D.05 0.04 S 03圖4-11弓形降液管的寬度和面積查圖 4-11,得 Wd/D =0.110 , Af/At =0.055

24、故 Wd =0.110 2.6 =0.286m22.2Af =0.055 D = 0.292mAt =5.31 m4由下式計(jì)算液體在降液管中停留時(shí)間以檢驗(yàn)降液管面積,即提：巳=心=冬地=16但湛符合要求Ls0.00791提：業(yè)二04邳s 符合要求Ls0.01764.1.2.4降液管底隙高度1精儲(chǔ)段ho= hw0. 00令 0. 0 4n4(2)提儲(chǔ)段ho =hw -0.006 = 0.034m4.1.2.5受液盤受液盤凹形和平形兩種,對(duì)于塔徑為800mm以上的塔,常采用凹形受液盤,這種結(jié)構(gòu)在低流量時(shí)仍能造成正液封,且有改變液體流向的緩沖作用.凹形受液盤的的深度一般在50mm以上.選用凹形受液盤

25、：深度 h =55mm三塔板布置1.取邊緣區(qū)寬度 Wc = 0.06m,安定區(qū)寬度 Ws = 0.085m2.依下式計(jì)算開孔區(qū)面積Aax=？-(Wi WS) = 6 -(0.198 0.08)m= 1.022mR = D 一雙二26. =1.24m 22A =2 xJr2 -x2R2sin A -180 R=2 1.022 .1.242匚1.0222 1.242 sin J1 = 4.41m2_1801.24其中圖4-8 塔板結(jié)構(gòu)參數(shù)其中:hw-出口堰局how堰上液層局度h,h1一進(jìn)口堰與降液管的水平距離hw進(jìn)口堰局HHt一板間距l(xiāng)w-一堰長(zhǎng)VWc-無效周邊局度ws-安定區(qū)寬度DR-一-鼓泡區(qū)

26、半徑x-鼓泡區(qū)寬度的1/2t-同一橫排的閥孔中央距(單位均為m)降液管底隙高度d降液管中活液層高度/d 弓形降液管高度塔徑(四) 篩孔數(shù)n與開孔率中3mm,取 t /d = 3 ,取篩孔的孔徑d.=5mm ,正三角形排列,一般碳鋼的板厚5 =故孔中央距t =3 5 = 15mm圖5-9篩孔的正三角形排列依下式計(jì)算塔板上的篩孔數(shù)n,即(1.155 )(1.155 )不n = Ao = ,2 伙 4.41 = 22638 II t )9015 )依下式計(jì)算塔板上的開孔區(qū)的開孔率甲,即4他=% =呼=10.8% (在5吩15泌圍內(nèi))At/do3每層塔板上的開孔面積A.為A.= A =0.1008 4

27、.41 =0.44m2精僻段：氣體通過篩孔的氣速蘭=迎6=16.加/A 0.44提僻段氣體通過篩孔的氣速 * =金=6274 =15.61 m/sA 0.44七、篩板的流體力學(xué)驗(yàn)算(一)氣體通過篩板壓強(qiáng)降的液柱高度 hp依式 hp = he n h._p e 11.精僻段：(1)干板壓強(qiáng)降相當(dāng)?shù)囊褐叨萮c依 d0/、 =5/3=1.67圖4-13干篩孔的流量系數(shù)查圖 4-13 , C.=0.78hc =0.051凸2(呈)=0.051 1613 = 0.036mC.0.78831.69(2) 氣流穿過板上液層壓強(qiáng)降相當(dāng)?shù)囊褐叨萮 lUa =AT Af7.0865.310.292= 1.41

28、m/sFa =ua 虧=1.41 .138=1.662.圖4-14充氣系數(shù)關(guān)系圖由圖4-14查取板上液層充氣系數(shù)8為0.58.依右式 f MhbW =0.58 0.07 = 0.041m(3) 克服液體外表張力壓強(qiáng)降相當(dāng)?shù)囊褐叨萮a依式(4-41 )4 40.86 10831.69 9.81 0.005=0.004m故hp1 =hc1 hnh；：.1 =0.036 0.041 0.004 =0.091 m單板壓強(qiáng)降 APP1 =hP1PL1g =0.081 乂 831.69 x 9.81 =0.6610.7kPa(設(shè)計(jì)允許值)提僻段(1)干板壓強(qiáng)降相當(dāng)?shù)囊褐叨萮c依 d0/、=5/3=1.

29、67查圖得,Co =0.78hc2 =0.051(4)2(與)=0.051 件宜CoPL10.7如 032.13 J=0.023m(2) 氣流穿過板上液層壓強(qiáng)降相當(dāng)?shù)囊褐叨萮 iUaAt -Af6.8695.310.292=1.37m/sFa=1.37 、應(yīng)=1.39由圖查取板上液層充氣系數(shù)8為0.61依右式 m =：hw how =0.58 0.07 = 0.041m(3) 克服液體外表張力壓強(qiáng)降相當(dāng)?shù)囊褐叨萮a344 58.43 10依式(4-41 ) h = 0.005m,：L1gdo932.13 9.81 0.005故hp2 =hc2 hl2 h廠2 = 0.023 0.043 0

30、.005 =0.071 m單板壓強(qiáng)降 APpi =hPPL1g =0.071 X932.13X9.81 =0.649 kPa 業(yè)=756.51皿施二0.00605m3/s 玲 881.91 3600那么dL4 0.00605 二 0.8利用液體的重力進(jìn)行回流,取適宜的回流速度uL=0.8m/s-0.098m經(jīng)圓整選取熱軋無縫鋼管,規(guī)格：力108X 5mm5.4.塔頂上升蒸汽管 塔頂上升蒸汽的體積流量:VSVVMV954.55 30.151.21 3600=6.61m3/s取適宜速度 UV=20m/s,那么 d = =J4,6.61 = 0.53muV；二 30經(jīng)圓整選取拉制黃銅管,規(guī)格：力540 x 5mm輔助設(shè)備的計(jì)算及選型1.冷凝器熱負(fù)荷逆流操作,那么按泡點(diǎn)回流設(shè)計(jì),即飽和蒸汽冷凝且飽和回流,采用30 C的水作為冷卻劑,Q=W r11=VM VDP1查液體的汽化潛熱圖,可知塔頂溫度 78.21 C下,乙醇汽化潛熱：rA =750KJ/kg水的汽化潛熱：rB=1750KJ/kgr1=E nxi=750 X 0.86X 46+ ( 1-0.86) X 1750X 18=34080KJ/Kmol故 Q=2085.37 X 34080/3600=1372.15KJ/s那么&(78.21 -30)-(78.